Lignin depolymerisation and doxygenation process for obtaining aromatic compounds and their catalytic reaction composition

ABSTRACT

The present invention is related to a catalytic process, which includes catalytic compositions for depolymerisation and deoxygenation of lignin contained in the biomass for obtaining aromatic hydrocarbons. The catalytic composition consists of at least one non-noble element from group VIIIB of the periodic table supported on a mesoporous matrix composed of an inorganic oxide, which can be alumina surface-modified with a second inorganic oxide with the object of inhibiting the interaction between the active component and the support. The process of lignin depolymerisation consists of dissolving lignin in a mixture of protic liquids, reacting it|a reaction system by batch or in continuous flow at inert and/or reducing atmosphere, at a temperature of between 60 to 320° C. and a pressure of from 5 to 90 kg/cm2. When the reaction is developed into a batch system, oxygenated aromatic hydrocarbons are mainly produced, both by thermal as well as catalytic depolymerisation, whereas in a continuous flow reaction system, deoxygenated aromatic hydrocarbons are produced.

TECHNICAL FIELD OF THE INVENTION

The current invention is related to the catalytic process including catalytic reactions for the depolymerisation and deoxygenation of lignins contained in the biomass for obtaining aromatic hydrocarbons. The catalytic composition consists of at least one non-noble element from group VIIIB of the periodic table supported in a mesoporous matrix composed of an inorganic oxide, which can be alumina surface modified with a second inorganic oxide with the object of inhibiting the interaction between the active component and the support. The process of lignin depolymerisation consists of dissolving lignin in a mixture of protic liquids, react it in a batch reaction system or in a continuous flow reaction system at inert and/or reducing atmosphere, at a temperature consisting of between 60 to 320° C. and a pressure of between 5 to 90 Kg/cm². Oxygenated aromatic hydrocarbons are mostly produced when the reaction is developed in a batch system, while deoxygenated aromatic hydrocarbons are produced in a continuous flow reaction system.

BACKGROUND OF THE INVENTION

Human activity is the main cause of global warming and climate change. To carry out his domestic, transport and industrial activities man requires of energy, which he satisfies by the combustion of fossil fuels and which generates great amounts of greenhouse effect gases. However, said activities that are associated with the emission of gases are essential for the world economy and form a fundamental part of modern life; therefore, there must exist a suitable balance between the growing energy demand and the urgent need to protect the environment and climate. Reason for which, there is the need to develop viable and sustainable novel energy sources, such as biorefinary technologies, which maximize the yield of renewable fuels, biological origin chemical products, and bioenergy. In fact, there have surged program policies and national plans in Europe as well as the United States of America, to develop bioenergy. The results indicate that the conversion of biomass to biofuels can give origin to a renewable and sustainable energy source for obtaining liquid fuels for transport.

Recent studies suggest that only in the United States of America 1.3 billion tons of biomass can be produced annually in a sustainable manner from agriculture and forestry. Which indicates that it can provide biomass as a raw material sufficiently to substitute at least 30% of the liquid fuels needs for transport in the U.S.A., without compromising its food production needs, by the suitable coupling of advanced technologies for the transformation of biomass with the changes in soil use. Even when the production of biofuels must yet overcome multiple technical and economical challenges, various cellulosic ethanol plants have been projected at a commercial level.

In first generation cellulosic bioethanol plants, great amounts of lignin will be produced as a by-product, from grains. This lignin is underutilized since about 60% more of it is produced than the amount required to satisfy the internal energy requirements of the plant by its combustion. Lignin is considered an affordable renewable source and of potential industrial use, whose annual production has been estimated to be in the range of 5-36×10⁸ annual tonnes worldwide. It is considered the second most abundant compound on Earth, after cellulose and its structure is composed mainly of phenylpropanoid units, which makes it the only renewable source of great volume composed mainly of aromatic hydrocarbons. Therefore, it is important to develop new processes for its transformation into chemical products of greater added value. Moreover, the department of energy of the United States of America has projected obtaining 79 billion litres per annum of second generation bioethanol (from agroindustrial residues) starting on 2022, for which about 223 million tons of biomass will be used annually and will produce about 62 million tons of lignin annually. Lignin produced as so will exceed by far the current needs of lignin in the world market for obtaining speciality products.

On the other hand, lignocellulosic materials coming mainly from agroindustrial residues contain between 15 and 30% lignin. Lignin is found forming an organic biopolymer, which envelops holocellulose (cellulose+hemicellulose). In order to take advantage of and convert cellulose and hemicellulose contained in the biomass to glucose and xylose, pentose and hexose, and subsequently to ethanol, it is necessary to extract the lignin contained in the biomass. Lignin contained in the biomass consists of an amorphous polymer containing in its structure great amounts of phenylpropanoid compounds, aromatic groups and methoxide groups and OH's, which must be used up for their transformation into chemical compounds of higher added value such as a renewable source to obtain aromatic hydrocarbons such as BTX fraction, vanillin, guaiacol, cresols, etc.

Lignin is an abundant source of renewable raw materials, being the future applications and perspectives very promising. However, although great amounts of lignin are produced, about 98% of this material is burnt directly into the same manufacturers in an energy recovery stage. Only 2% is commercially exploited. It seems that during the next few years this will be a promising field for obtaining chemical products with high added value. Thus, lignin represents a renewable and potentially valuable source for obtaining chemical compounds mainly of the aromatic type. Therefore, it represents an opportunity to develop chemical and biological processes for the degradation of the biopolymer, which could be used both for holocellulose decomposition and the production of biofuels, as well as to generate aromatic chemical products from lignin. And so, form the basis of a “bio-refinery”.

Lignin is a heterogeneous mixture of aromatic polymers, which are rigid and resistant, and serve to protect the polysaccharides in the cell walls from degradation and chemical attacks. The content of lignin in the biomass varies depending on the origin of the biomass: soft woods have between 25-35% weight, while the herbaceous biomass contains between 14-20% weight. The most important challenge to give value to lignin resides in selectively breaking the C—O linkages to produce simpler aromatic compounds, appropriate to integrate into petrols, to be used as chemicals per se or as precursors for their transformation into products of higher added value. Although the advances in the conversion of lignin into high added value chemicals and biofuels, its combustion to generate energy is still favoured and, commercially, is its only viable use, until today. Therefore, the object of this patent is to establish a catalytic process, which allows transforming lignins and agroindustrial residues, lingo-cellulosic renewable sources, into chemical products of high added value, maximizing the yield to aromatic compounds and phenols.

BRIEF DESCRIPTION OF THE FIGURES

With the purpose of having an understanding of the lignin depolymerisation and deoxygenation process for obtaining aromatic compounds and its catalytic reaction composition, objects of the present invention, reference will be made to the accompanying figures, without limiting its scope:

FIG. 1 shows an illustrative chromatogram of the different products obtained after the lignin depolymerisation reaction.

FIG. 2 shows an illustrative chromatogram of the different products obtained after the lignin depolymerisation and deoxygenation reaction.

DETAILED DESCRIPTION OF THE INVENTION

This invention is related to a catalytic process, which includes catalytic compositions for the depolymerisation of lignins contained in the biomass for obtaining aromatic hydrocarbons. The process consists of submitting lignin to a hydrothermal and/or solvothermal treatment in a protic liquid, with or without a catalyst with the object of solubilizing lignin, eliminating inorganic solids and solid impurities contained therein, and depolymerising or partially fragmenting lignin into its different monoaromatic units. Partially depolymerised lignin soluble in a protic liquid is obtained from this process, which afterwards passes through a fixed bed reactor packed with a catalytic composition, also object of the present invention, to obtain a mixture of oxygenated and/or partially deoxygenated aromatic compounds contained in the protic solvent.

The catalytic compositions, object of the present invention, consist of a mixed oxide, which can contain alumina and/or silica and can contain or not, at least one non-noble metal element of the VIIIB group of the periodic table deposited in its surface, to increase the density of active sites for the hydrotreating and hydrodecarboxylation reactions, specifically hydrodeoxygenation or decarboxylation of the oxygenated aromatic hydrocarbons produced during depolymerisation.

Therefore, the present invention provides an aluminium oxide material which serves as a catalyst and/or alumina support from a boehmite-phase precursor, which is formulated in cylindrical, trilobal or tetralobular extrudes with resistance to fracture superior to 3 Ibf/mm by the addition of a solution containing an organic or inorganic acid to formulate the paste with suitable consistency to be extruded. Once the extrudes are obtained, they are dried and burnt at temperatures higher to 400° C. to obtain the support in alumina-phase extrudes. The obtained extruded is subjected to a surface modification process consisting of the impregnation of an inorganic oxide with a concentration of less than or equal to 15% by weight and it is subsequently burnt at a temperature of over 400° C., thereby obtaining a support and/or catalyst with surface characteristics and acid properties suitable for the lignin depolymerisation reaction and for preparing catalysts containing at least one non-noble metal component of the VIIIB group of the periodic table as active phase for the lignin depolymerisation and deoxygenation process.

In this regard, it is worth pointing out that the obtained aluminium oxide material has improved textural properties by increasing the diameter and volume of the pore, which serve as catalyst and/or alumina-based catalyst support obtained from an aluminium oxyhydroxide precursor, preferably of bohemite phase, which peptizes with an inorganic acid, reacting the aluminium oxyhydroxide with an aqueous solution containing an inorganic acid at a molar concentration of 0.01 to 1 M; subsequently, the peptized oxyhydroxide material is reorganised around a surfactant of high volume, preferably of neutral character, by the addition of said surfactant to the solution. During this process, the aluminium oxyhydroxide nanoparticles are peptized and partially dissolved. Afterwards, it is left to cool at a temperature of between 20 and 40° C. and a neutral surfactant is added, a three-block type copolymer forming micelles in the solution, around which the peptized aluminium oxyhydroxide nanoparticles are reorganized and it is left stirring for 4 to 36 hours. A surfactant/aluminium oxyhydroxide ratio was used comprising from 0.1 to 10. Finally, the material is dried at a temperature of between 50 and 120° C. for a time of between 12 and 72 hours. Subsequently, the surfactant is removed from the obtained material by burning at air atmosphere, passing an air flow comprising from 20 to 100 cm³/minute for 4 to 12 hours. The resulting solid is subjected to a surface modification process consisting of the impregnation of an inorganic oxide at a concentration of less than or equal to 15% by weight and its subsequent burning at a temperature of over 400° C., thereby obtaining a support and/or catalyst with surface features and acid properties suitable for the lignin depolymerisation reaction and for preparing catalysts containing at least one non-noble metal component of the VIIIB group of the periodic table as active phase for the process of lignin depolymerisation and deoxygenation.

The mesoporous alumina support with pore diameters superior to 15 nm can be subjected to a process of extraction before or after its surface modification with inorganic oxide, by the addition of a solution containing an organic or inorganic acid to formulate the paste with suitable consistency to be extruded. The obtained paste is formulated in cylindrical, trilobal or tetralobular extruded. Once the extruded are obtained, they are dried and burnt at temperatures higher than 400° C. to obtain the support in alumina-phase extruded or surface-modified alumina with inorganic oxide. If the obtained extruded has not been surface modified with an inorganic oxide, it is subjected to a surface modification process consisting of the impregnation of an inorganic oxide at a concentration of less than or equal to 15% by weight and its subsequent burning at a temperature above 400° C., thereby obtaining a support and/or catalyst with surface features and suitable acid properties for the lignin depolymerisation reaction and for the preparation of catalysts containing at least one non-noble metal component of the VIIIB group of the periodic table as active phase for the lignin depolymerisation and deoxygenation process.

An object of the present invention is to obtain active catalysts for lignin depolymerisation and hydrodeoxygenation by impregnation in incipient wet of at least one non-noble metal component of the VIIIB group of the periodic table, which consists in dissolving a precursor salt of the metal element in a protic solvent at such a concentration which allows obtaining a concentration comprised between 2 and 20% by weight of the metal element in the final solid. The metal component of the VIIIB group of the periodic table can be nickel, cobalt or iron, and the precursor salt of said metal component can be chlorine, nitrate, acetate, carbonate or hydroxycarbonate, etc. and the protic liquid can be water or any alcohol such as methanol, ethanol, 1-propanol or isopropanol, 1-butanol, etc.

The impregnation method by incipient wet consists of contacting the solution containing the precursor salt of the metal element of the VIIIB group of the periodic table with the formulated support in cylindrical, trilobal or tetralobular extruded, modified with an inorganic oxide and previously dried in an oven at 110° C., until all the solution is absorbed by filling in the volume of pores of said support. Afterwards, it is left standing keeping the surface of the support wet with said solution for a period of time of 12 to 18 hours. Subsequently, it is dried at 110° C. and it is burnt at a temperature comprised between 400 and 600° C. in air atmosphere, passing air fluid comprising between 20 to 100 cm³/minute for 4 to 12 hours.

An embodiment of the process of the present invention is the lignin thermal and/or catalytic depolymerisation process by a liquid reformation process with a protic solvent or mixture of solvents in a reactor by autoclave-type batches. Said process consists of dissolving lignin in a mixture of protic solvents, basically in alcohol-water at a ratio comprised of 10:90 to 90:10 vol:vol, when lignin is soluble in protic solvents, or when lignin is insoluble, the insoluble solid is added to the mixture of protic solvents and the temperature is increased to dissolve and reach the reaction temperature. Soluble or insoluble commercial lignin can be used as a lignin source, such as sodium lignosulfonate, alkaline Kraft lignin, organosolv lignin, lignin obtained from any lignocellulosic residue as a cellulose and hemicellulose hydrolysis by-product in order to produce alcohols, and/or residue waste by-products named “black liqueur” of the paper industry, and/or the same biomass or lignocellulosic agroindustrial residue rich in lignin, such as wood chip, sugar cane bagasse, agave bagasse, etc. The alcohol used as protic solvent can be any primary or secondary alcohol, such as methanol, ethanol, propanol, isopropanol, 1-butanol, 2-butanol etc., preferably methanol or ethanol. The amount of lignin or black liqueur or biomass as lignocellulosic residue is between 10 to 250 g/L, preferably from 10 to 150 g/L. To carry out a thermal reaction the solution containing lignin is loaded onto an autoclave, sealed tightly, a test for leakages is carried out and the oxygen present is removed by nitrogen scanning twice and the stirring is started at 250 rpm. Afterwards, the heating is started with a ramp of from 1 to 10° C./min until reaching the reaction temperature of between 80 to 300° C. Once the reaction temperature is reached, the pressure is configured with an inert gas or with a reducing gas until reaching a pressure in the system of between 30 and 90 kg/cm². Finally, it is left to react for a reaction time of between 0.5 to 4 hours, preferably of between 0.3 and 2 hours.

Once the reaction period is finished, the liquid containing the depolymerised lignin is filtered to remove non-transformed solids, solid residues and/or catalyst. Afterwards, the separation process of the depolymerised organic compounds containing mainly aromatic compounds is carried out by the addition of an aprotic polar solvent and vigorous stirring of the resulting liquid, with which the separation of two phases is carried out. The liquid is placed in a separation funnel by which an organic fraction and an aqueous fraction are separated. In the organic fraction, the resulting aromatic organic compounds are dragged from the lignin depolymerisation, which can contain both oxygenated and deoxygenated aromatic compounds, and other organic compounds such as alcohols, ketones, naphthenes, olefins, paraffin, carboxylates, carboxylic acids, etc. and in the aqueous fraction, dissolved non-reacted lignin is mainly found, small quantities of hydrocarbons which were not extracted with the aprotic polar solvent, inorganic salts contained in the lignin of origin.

The aprotic polar solvent, which is used for the recovery of the organic compounds of the reaction products coming from the reactor by autoclave-type batches, can be selected from tetrahydrofuran or dichloromethane, preferably dichloromethane, since it shows a lower boiling temperature, of about 40° C. Once the organic fraction is separated it is subjected to a distillation process at the boiling temperature of the aprotic polar solvent with the object of recovering the solvent used for the extraction of the organic compounds, and afterwards it is distilled at the temperature of the alcohol used for the reaction with the object of removing the alcohol fraction which is dragged in the aprotic polar solvent, said temperature is from between 60 and 100° C. The resulting liquid product of the reaction was analysed in a gas chromatograph coupled to a mass spectrometer, with which the identification of the different compounds present was carried out. FIG. 1 shows an illustrative chromatogram of the different products obtained after the lignin depolymerisation reaction. The aqueous fraction is distilled at a temperature of 100° C., in order to remove all water and thereby recover the dissolved solid, with the object of determining the percentage weight of lignin converted into products. The selectivity is determined by considering the area below the curve of each chromatographic peak identified with a probability assignment greater than 80, and the peaks not identified with said probability were grouped as non-identified compounds.

Another embodiment of the process of the present invention is the realization of the lignin thermal and/or catalytic depolymerisation reaction by a process in continuous flow, which consists of a pre-treatment section of the feeding load which at the same time consists of the lignin dissolution in a mixture of protic solvents, basically in alcohol-water at a ratio comprising 10:90 to 90:10 vol:vol, when the lignin is soluble in protic solvents, afterwards and with object of removing all cations and anions of the inorganic compounds present in lignin, said components are contacted with cationic and anionic interchange resins consecutively, with which inorganic cations are removed such as sodium, potassium, calcium, silicon, etc., and anions such as sulphates, nitrates, chlorides, etc. Once the inorganic cations and anions are removed, the lignin solution is pumped to a reactor wherein it is contacted with the catalyst, in the case of the reaction being catalytic; and for the thermal reaction the reactor is packed with silicon carbide and therefore the lignin solution is contacted with the silicon carbide.

The process in continuous flow consists of a reaction section composed of a tubular reactor packed with an inert material when the reaction is carried out by a thermal reaction or with a catalyst, in the case of the reaction being carried out with a catalyst. The catalyst and/or silicon carbide are loaded onto the reactor with a granulometry comprising from 200 microns up to 2.0 mm, be it mechanically grinded or directly into cylindrical, trilobal or tetralobular extruded. Before feeding the reacting lignin solution, the catalyst is activated by a reduction process, which consists of heating the reactor in presence of a reducing gas at high pressure. The reactor is heated at a temperature of between 300 to 500° C., with a reducing gas flow, preferably hydrogen of 3 to 8 L/hour maintaining a pressure in the reactor of between 30 to 90 kg/cm². Once the catalyst is activated, the solution containing the resulting lignin is passed through the reactor at a flow speed comprising between 5 and 50 mL/hour, in order to maintain the spatial temperature of the liquid with regards to the catalyst volume (LHSV, liquid hourly space velocity) comprised of between 0.5 and 10 hr⁻¹. The lignin depolymerisation reaction can be carried out with inert gas flow or with a gas or reducing agent. When it is carried out with inert gas flow, an inert gas is passed which can be nitrogen, helium, argon, and/or a mixture thereof at a flow speed comprising between 1 and 10 L/h, keeping a pressure comprising between 30 and 90 kg/cm². When the reaction is developed with a reducing agent, a hydrogen flow is passed at a flow speed comprising between 1 and 10 L/h, keeping a pressure of between 2 and 30 kg/cm².

The recovery of the reaction products is carried out in a condenser placed on the outlet of the reactor wherein the liquid effluents are condensed at room temperature, and it is separated from the gases generated during the reaction. The generated gases are analysed by a gas chromatograph connected in line and the liquid effluents are recovered for their subsequent treatment and analysis to identify the reaction products.

When the reaction is carried out with inert gas, the products identified in the reaction gases are hydrogen, carbon monoxide, carbon dioxide, oxygen and C₁-C₆ hydrocarbons, paraffin, isoparaffin, olefins, isooleffins, etc. When the reaction is carried out in hydrogen flow, the reaction gases are composed mainly of carbon dioxide, carbon monoxide, C₁-C₆ hydrocarbons, paraffin, isoparaffin, olefins, isooleffins, etc.

The resulting liquid products of the reaction consist of a crystalline solution slightly yellow transparent, which is indicative of it not containing non-transformed lignin and that lignin has been depolymerised into simpler chemical compounds. When lignin is found without transformation, it generally consists of a black colour dark solution; in fact, the lignin solution fed to the system consists of a black colour dark solution, and the reaction product derived therefrom is transparent of clear yellow colour.

The liquid fraction containing the reaction products is subjected to a separation procedure of the depolymerised organic compounds, which mainly contain aromatic compounds, by the addition of an aprotic polar solvent and a vigorous stirring of the resulting liquid, with which the two-phases separation is carried out. The liquid is placed in a separation funnel by which an organic fraction and an aqueous fraction are separated. In the organic fraction the resulting aromatic organic compounds are dragged from the lignin depolymerisation, which can contain both oxygenated and deoxygenated aromatic compounds, and other organic compounds such as alcohols, ketones, naphthenes, olefins, paraffin, carboxylates, carboxylic acids, etc., and in the aqueous fraction, non-reacted lignin is mainly found dissolved, small amounts of hydrocarbons which were not extracted with the aprotic polar solvent, inorganic salts contained in the lignin of origin. When the total conversion of lignin is reached, the aqueous fraction resulting from the separation is crystalline, transparent and colourless, indicating that there is no lignin dissolved therein. For the recovery of reaction products in the continuous flow process, an extraction treatment with an aprotic polar solvent is carried out in the same manner as for the reaction products of the reactor by autoclave-type batches, for the separation of organic compounds from the aqueous fraction, as described above. FIG. 2 shows an illustrative chromatogram of the different products obtained after the lignin depolymerisation and deoxygenation reaction in a fixed bed and continuous flow reactor.

Now we mention some of the compounds obtained by the process of the present invention under its two embodiments, but that are in no way exclusively limited thereto: a) identified non oxygenated aromatic compounds are: toluene, ethyl benzene, para-xylene, meta-xylene and ortho-xylene, trimethyl-benzene, ethyl-methyl benzene, propyl-ethyl benzene, generally di- and trialkyl-benzenes; b) oxygenated aromatic compounds are: phenol, 2-metoxyphenol, 4-methyl-2-metoxyphenol, 2,6-dimetoxyphenol, 1,2-dimetoxybenzene, 4-ethyl-2-metoxyphenol, 4-propyl-2-metoxyphenol, etc.

REFERENCES

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EXAMPLES

Now the invention will be further described by reference to examples related to the lignin depolymerisation and deoxygenation process for obtaining aromatic compounds and their catalytic reaction composition, objects of the present invention and previously described, without them limiting the scope of the present invention.

Thermal and catalytic depolymerisation experiments on lignin Kraft were carried out in ethanol-water at temperatures of 60 to 290° C., at a pressure of 2,413 to 8,274 kPa (350 to 1200 psi), and lignin/solvent ratios (ethanol+water) of 2 to 20 g/L.

Example 1. Preparation of Cylindrical Particles (Extruded) Gamma-Alumina Phase (EA)

Supports of gamma-Al₂O₃ formulated in the form of cylindrical particles were obtained from an alumina-hydrated precursor (commercial bohemite), for which the bohemite powder material is dried at 110° C. for 20 hours, it is sifted using a mesh EE.UU. 100, with an opening of 0.149 mm, to homogenize the particle size. In order to formulate the extruded, 500 g of powdered material bohemite phase was used, which was placed on a mixer (Bench Kneader, Mod. PNV-1) slowly adding 100 mL of a HNO₃/H₂O solution at 1% mol, for a period of 2.5 hours, without interrupting the mixing, by which a moist paste of bohemite is formed of uniform consistency and malleable at the same time, this paste was introduced into an extruder (DOTCO, Mod. BA-293), using compressed air at a pressure of 1,100 kPa; the obtained extruded had cylindrical and trilobal form of 1/16″ diameter. Said extruded were left standing at room temperature (25° C.) for a period of time of between 18 and 24 hours; afterwards, they were subjected to a drying process on a convection oven, firstly at a temperature of 60° C. for 4 hours, afterwards the temperature was increased to 80° C. for 5 hours, and lastly the temperature was increased to 120° C. for 16 hours. For the burning of the extruded, a heating ramp was used of 5° C./min up to 550° C. staying at these conditions for 4 hours under air flux of 150 mL/min. The X ray analysis shows that the crystalline phase of the extruded obtained after the burning corresponds to the gamma-alumina. The textural properties of this support (SAS) showed a specific area of 300 m²/g, pore volume of 0.74 cm³/g and average pore diameter of 9.9 nm.

Example 2. Preparation of Cylindrical Particles (Extruded) Gamma-Alumina Phase Modified with Silica According to the Invention (EAS)

In order to prepare the EAS support, the EA support prepared in Example 1 was used. The EA support in the form of previously burnt extruded, was dried in the oven at 120° C. for two hours, afterwards it was modified with 5% by weight of SiO₂ by the following procedure:

In a 3 L flask anhydrous ethanol is mixed with tetra-ethyl-orthosilicate (TEOS, SiC₈H₂₀O₄), using magnetic stirring. Afterwards, the temperature in the flask is increased up to 70° C. and it is maintained at reflux for 1 hour. Then, it is cooled at 25° C. When this temperature is reached, the hydrolysis of the TEOS is used using slow drop-by-drop of a mixture of anhydrous ethanol, water and nitric acid, with a molar ratio of H₂O/TEOS=4, ethanol/TEOS=40 y HNO₃/TEOS=0.1.

After adding the hydrolysis solution, it is left stirring for 30 minutes at room temperature (25° C.). Afterwards, the alumina support extruded previously dried in an oven at 120° C. are added and it is left standing for 12 hours at room temperature. Then, the filtration of the TEOS-modified support is carried out and the extruded are dried at 120° C. for a period of 18 hours. Finally, the extruded are burnt in air flow at 400° C. for 18 hours. The final composition of the extruded support gamma-alumina phase modified with silica was: 0=48.39% by weight, AL=48.06% by weight and Si=3.55% by weight, and its textural properties show an specific area of 275 m²/g, pore volume of 0.61 cm³/g and pore diameter of 8.9 nm.

Example 3. Preparation of Cylindrical Particles (Extruded) Mesoporous Gamma-Alumina Phase (EAS Meso)

12 g of pseudobohemite were peptized (AlOOH) with a nitric acid solution 0.334 M. To the obtained suspension, Pluronics P-123 surfactant was added and was left shaking for 24 hours at room temperature. A surfactant/AlOOH (w/w) ratio=2, was used. Afterwards, the obtained mixture was dried at 50° C. for 24 hours and afterwards at 90° C. for 24 hours; finally, the obtained material was thermally treated with air flow of 100 mL/min to remove surfactant, using a ramp of 1° C./min up to 300° C./min for 4 hours and afterwards from 1° C./min up to 500° C. for 6 hours.

Afterwards, the material was meshed above 100 mesh (<160 μm) and dried at 110° C., and for its moist extrusion, the powder was mixed with a citric acid solution at 1% by weight. The paste was formulated in cylindrical extruded of a 1/16″ diameter, first drying at room temperature for 24 hours; and then drying at 60° C. for 4 hours, 80° C. for 5 hours and at 100° C. for 12 hours. Immediately, it was thermally treated at 1° C./min up to 500° C. for 6 hours in air flow using air flow at 150 mL/min.

Subsequently, silica is added (via TEOS) to obtain the extruded (5% weight of SiO₂) by the procedure used in Example 3.

Example 4. Preparation of the Zeolite Phase Material (MMZ-112C, MMZ-113C and MMZ-114C)

The preparation of zeolites was carried out as described in the patents (MX320407, EP 2 570 386 B1). The materials MMZ-112C, MMZ-113C, MMZ-114C, were prepared by the depolymerisation method at 200, 225 and 180° C., respectively. In all cases the recrystallization was carried out at a temperature of 150° C. and were burnt at 550° C. for a period of 6 hours.

Example 5. Preparation of Cylindrical Particles (Extruded) Extruded Material Alumina-Silica-Zeolite Phase (ExMMZ-112C)

To 5.79 g of EAS, 5.2 mL of 5% HNO₃/H₂O were added until having a moist paste, afterwards 5.4 mL of H₂O were added. To this paste 15 g of MMZ-112C+16 mL H₂O, were added. 0.55 g of Ludox-TMA and 0.5 g of ethyl-methyl-cellulose (EMC, Dow Corning) were added in the form of gel adding with 1.9 mL water. The resulting moist paste was stable for extrusion. This material in the form of cylindrical extruded presents an specific area (Langmuir) of 652 m²/g, an specific area (microporous) of 543 m²/g, total pore average volume of 0.399 cm³/g and a pore diameter of 15.57 (A).

Example 6. Preparation of Cylindrical Particles (Extruded) Extruded Material Alumina-Silica-Zeolite Phase (ExMMZ-113C)

First, 0.513 g of ethyl-methyl-cellulose (EMC, Dow Corning) were gelled with 2.9 mL of 5% volume HNO₃/H₂O, and afterwards 10.5 g of EAS in powder+15.9 mL of 5% volume HNO₃/H₂O, were added. Once the moist paste was formed, 4.5 g of MMZ-113C were added to obtain a lumpy mixture. Moreover, 2.0 mL of deionized water were added to for a malleable and stable paste. The extrusion was carried out using a diameter of 1/16″. This material in the form of cylindrical particles presents a specific area (Langmuir) of 464 m²/g, a specific area (microporous) of 237 m²/g, total pore average volume of 0.62 cm³/g and pore diameter of 73 (Å).

Example 7. Preparation of Cylindrical Particles (Extruded) Extruded Material Alumina-Silica-Zeolite Phase (ExMMZ-114C)

First, 0.503 g of ethyl-methyl-cellulose (EMC, Dow Corning) were gelled with 3.0 mL 5% volume HNO₃/H₂O, and 10.5 g of EAS in powder+16.5 mL of 5% volume HNO₃/H₂O were added afterwards. Once the paste was formed, 4.5 g of MMZ-114C were added to again have a lumpy mixture. 2.0 mL of deionized water were added additionally to forma malleable and stable paste. The extrusion was carried out with a diameter of 1/16″. This material in the form of cylindrical particles presents a specific area (Langmuir) of 536 m²/g, a specific area (microporous) of 327 m²/g, total pore average volume of 0.75 cm³/g and pore diameter of 77 (Å).

Example 8. Preparation of Catalyst 15Ni-EAS

The impregnation solution was prepared by dissolving 10.3 g of nickel nitrate Ni(NO₃)₂.6H₂O, in 77.6 mL of water double-distilled with stirring. Once the nickel was dissolved the solution turned transparent green. Afterwards, the solution was concentrated to a suitable volume to be used in the impregnation of 17.65 g of support EAS to fill in the pores. The amount dissolved salts varies based on the metal concentration desired to be obtained in the final solid which was of 15% weight nickel, the material was taken to a drying process at 120° C. for a period of 12 hours and afterwards the burning in air flow at a temperature of 400° C. for 4 hours. The catalyst was labelled as 15Ni-EAS.

Example 9. Preparation of the Catalyst 15Co-EAS

The impregnation solution was prepared by dissolving 8.8 g of cobalt acetate C₄H₆CoO₄.4H₂O, in 25 mL water double distilled with stirring. Once the cobalt was dissolved, the solution turned wine red. Afterwards, the solution was concentrated at a suitable volume to be used in the impregnation of the EAS support to fill in pores. The amount of salts dissolved varies based on the concentration of metals desired to be obtained in the final solid, which was of 15% by weight of cobalt, the material was taken to a drying process at 120° C. for a period of 12 hours and afterwards to the burning in air flow at a temperature of 400° C. for 4 hours. The catalyst was labelled as 15Co-EAS.

Example 10. Preparation of the Catalyst 15Ni-EASMeso

The impregnation solution was prepared by dissolving 10.3 g of nickel nitrate Ni(NO₃)₂.6H₂O, in 77.6 mL of water double-distilled with stirring. Once the nickel was dissolved the solution turned transparent green. Afterwards, the solution was concentrated up to a suitable volume to be used in the impregnation of 17.65 g of support EAS by filling in pores. The amount of dissolving salts varies based on the concentration of metals desired to be obtained in the final solid which was of 15% by weight of nickel, the material was taken to a drying process at 120° C. for 12 hours, and afterwards a burning in air flow at a temperature of 400° C. for 4 hours. The catalyst was labelled as 15Ni-EASMeso.

Example 11. Preparation of Catalyst 15Ni-ExMMZ-112C

The impregnation solution was prepared dissolving 8.75 g of nickel nitrate Ni(NO₃)₂.6H₂O in 66 mL of water double-distilled with stirring. Once the nickel was dissolved, the solution turned transparent green. Afterwards, the solution is concentrated at a suitable volume to be used in the impregnation of 13.2 g of support ExMMZ-112C to fill in pores. The amount of dissolved salts varies based on the concentration of metals desired to be obtained in the final solid which was of 15% by weight of nickel; the material was taken to a drying process at 120° C. for a period of 12 hours and afterwards the burning in air flux at a temperature of 400° C. for 4 hours. The catalyst was labelled as 15Ni-ExMMZ-112C.

Table 1 shows all catalysts prepared with metal and without metal, objects of the present invention as well.

TABLE 1 Preparation of supports and catalysts. Metal (% weight) Catalyst Support Ni Co Example EA Al₂O₃ — 1 EAS Al₂O₃—Si — 2 EASMeso Al₂O₃ mesoporous-Si 3 MMZ-112C Zeolite mesoporous — 4 MMZ-113C Zeolite mesoporous 4 MMZ-114C Zeolite mesoporous 4 ExMMZ-112C Zeolite meso-Al₂O₃—Si 5 ExMMZ-113C Zeolite meso-Al₂O₃—Si 6 ExMMZ-114C Zeolite meso-Al₂O₃—Si 7 15Ni-EAS Al₂O₃—Si 15 — 8 15Co-EAS Al₂O₃—Si — 15 9 15Ni-EASMeso Al₂O₃ mesoporous-Si 15 — 10 15Ni-ExMMZ-112C Zeolite meso-Al₂O₃—Si 15 — 11 15Ni-ExMMZ-113C Zeolite meso-Al₂O₃—Si 15 — 12 15Ni-ExMMZ-114C Zeolite meso-Al₂O₃—Si 15 — 13 CMA Commercial reference catalyst alumina-Zeolite base

Example 12. Preparation of the Catalyst 15Ni-ExMMZ-113C

The impregnation solution was prepared dissolving 8.75 g of nickel nitrate Ni(NO₃)₂.6H₂O in 66 mL of water double-distilled with agitation. Once the nickel was dissolved the solution is turned transparent green. Afterwards, the solution is concentrated to a suitable volume to be used in the impregnation of 13.2 g of support ExMMZ-113C to fill in pores. The amount of dissolved salts varies based on the concentration of metals desired to be obtained in the final solid which was of 15% by weight of nickel, and the material was taken to a drying process at 120° C. for a period of 12 hours and then to a burning in air flow at a temperature of 400° C. for 4 hours. The catalyst was labelled as 15Ni-ExMMZ-113C.

Example 13. Preparation of Catalyst 15Ni-ExMMZ-114C

The impregnation solution was prepared dissolving 8.75 g od nickel nitrate Ni(NO₃)₂.6H₂O in 66 mL of water double-distilled water with stirring. Once the nickel was dissolved, the solution turned transparent green. Afterwards, the solution was concentrated to a suitable volume to be used in the impregnation of 13.2 g of support ExMMZ-114C to fill in pores. The amount of dissolved salts varies based on the concentration of metals desired to be obtained in the final solid which was of 15% by weight of nickel; the material was taken to a drying process at 120° C. for a period of 12 hours and then a burning in air flow at a temperature of 400° C. for 4 hours. The catalyst was labelled as 15Ni-ExMMZ-114C.

Example 14. Thermal Assessment of Lignin Kraft at 60° C. with Water/Ethanol Ratio (v/v) of 50/50

The thermal assessment was carried out at 60° C. in a batch-type reactor (Reactor Parr 4842) with a 250 mL capacity. The water/ethanol ratio (v/v) was 1.2 (50 mL water/50 mL ethanol). 2 g of lignin Kraft was used during reaction tests under a 4,137 kPa (600 psi) hydrogen pressure with mechanical stirring at 1000 rpm. Once said conditions were reached, the reaction is left for a period of 3 hours. The autogenous pressure reached was of 8,274 kPa (1200 psi).

When the reaction was completed, the reactor was disassembled from the heating systems to be immediately cooled.

The reaction product was treated under the following methodology:

-   -   1) Filter the reactor contents in a kitasato flask and filter         paper (Whatman brand number 2, that is, for a medium filter).     -   2) The liquid reaction mixture (ethanol-water) was placed in a         separation funnel. The organic phase contains the lignin         depolymerisation products. The aqueous phase contains unreacted         lignin.     -   3) Over the filtration funnel, 100 mL of dichloromethane (DCM)         are added so as to wash the solids contained in the filter         paper.     -   4) Afterwards the liquid mixture is poured in a separation         funnel and the phases are separated (aqueous and organic).     -   5) Two further washes are carried out, using 50 mL DCM in the         aqueous phase left over in the separation funnel, so as to         complete the extraction of the organic phase.     -   6) The aqueous phase contained in the funnel is preserved for         its further analysis in a gas chromatograph coupled to a mass         spectrometry detector and library NIST/EPA/NIH Mass Spectral         Search Library V2.0f (GC-MS, GC7820A-MSD 5975, Agilent         Technologies).     -   7) On the other hand, the final organic phase is placed on a         rotary evaporator. First it is heated at 40° C. at 50 rpm to         separate DCM.     -   8) Afterwards, it is heated at 85° C. at 50 rpm and then in         another container the ethanol contained in the sample is         separated.     -   9) The liquid product of the final organic phase is placed in a         flask for its further analysis in a GC-MS chromatograph.     -   10) The solid contained in the filter paper is placed in the         over at 120° C., for a period of 24 h, and then it is weighted,         to quantify the conversion by weight.     -   11) The lignin conversion was determined as follows:         X_(lignin)=(Initial weight−Final weight)*100/Initial weight. The         initial and final weight of lignin is dry base.

The lignin conversion was of 0.5% by weight. The reaction products, which are generated in greater amounts, are vanillin, aceto-vanillin and 4-hydroxy-3-methoxybenzeneacetic acid.

Example 15. Thermal Assessment of Lignin Kraft at 80° C. with Water/Ethanol Ratio (v/v) of 50/50

The thermal assessment was carried out at 80° C. in a batch-type reactor (Reactor Parr 4842) with a 250 mL capacity, under the same methodology as forth in Example 14. The lignin conversion was of 3.8% by weight. The reaction products generated in greater amounts are vanillin, aceto-vanillin and 4-hydroxi-3-methoxybenzeneacetic acid.

Example 16. Thermal Assessment of Lignin Kraft at 140° C. with Water/Ethanol Ratio (v/v) of 50/50

The thermal assessment was carried out at 140° C. in a batch-type reactor (Reactor Parr 4842) with a 250 mL capacity, under the same methodology as forth in Example 14. The lignin conversion was of 11.5% by weight. The reaction products generated in greater amounts are guaiacol, vanillin and aceto-guaiacona.

Example 17. Thermal Assessment of Lignin Kraft at 220° C. with Water/Ethanol Ratio (v/v) of 50/50

The thermal assessment was carried out at 220° C. in a batch-type reactor (Reactor Parr 4842) with a 250 mL capacity, under the same methodology as forth in Example 14. The lignin conversion was of 39.7% by weight. The reaction products generated in greater amounts are guaiacol, p-ethyl-guaiacol, p-propyl-guaiacol, aceto-guaiacol, homovanilic acid, vanillin, isoeugenol, creosol. FIG. 1 shows a chromatogram with products distribution and retention time.

Example 18. Thermal Assessment of Lignin Kraft at 260° C. with Water/Ethanol Ratio (v/v) of 50/50

The thermal assessment was carried out at 260° C. in a batch-type reactor (Reactor Parr 4842) with a 250 mL capacity, under the same methodology as forth in Example 14. The lignin conversion was of 53.4% by weight. The reaction products generated in greater amounts are the same as in Example 17. FIG. 1 shows a chromatogram with the products distribution and retention time.

Example 19. Thermal Assessment of Lignin Kraft at 290° C. with Water/Ethanol Ratio (v/v) of 50/50

The thermal assessment was carried out at 290° C. in a batch-type reactor (Reactor Parr 4842) with a 250 mL capacity, under the same methodology as forth in Example 14. The lignin conversion was of 59% by weight.

The activation energy calculated based on Examples 14, 15, 16, 17, 18 and 19 was of 7.05 kcal/mol (29.52 kJ/mol). The reaction products generated in greater amounts are the same as in Example 17. FIG. 1 shows a chromatogram with products distribution and retention time.

Example 20. Thermal Assessment at 290° C. of Lignin Kraft with Water/Ethanol Ratio (80/20)

The thermal assessment was carried out at 290° C. in a batch-type reactor (Reactor Parr 4842) with a 250 mL capacity. The water/ethanol ratio (v/v) was 80/20. 2 g of lignin Kraft was used in the reaction test under a 4,137 kPa (600 psi) hydrogen pressure with mechanical stirring at 1000 rpm. Once said conditions were reached the reaction is left for a period of 3 hours. When the reaction is completed, the reactor is dissembled from the heating system to be cooled immediately. The reaction product was treated under the same methodology used in Example 14. The lignin conversion was of 48% by weight. The reaction products generated in greater amounts are the same as in Example 17. FIG. 1 shows a chromatogram with products distribution and retention time.

Example 21. Thermal Assessment at 290° C. of Lignin Kraft with Water/Ethanol Ratio (20/80)

The thermal assessment was carried out at 290° C. in a batch-type reactor (Reactor Parr 4842) with a 250 mL capacity. The water/ethanol ratio (v/v) was 20/80. 2 g of lignin Kraft was used in the reaction test under a 4,137 kPa (600 psi) hydrogen pressure with mechanical stirring at 1000 rpm. Once said conditions were reached the reaction is left for a period of 3 hours. When the reaction is completed, the reactor is dissembled from the heating system to be cooled immediately. The reaction product was treated under the same methodology used in Example 14. In this case the lignin conversion was of 58% by weight, to the reaction timings. The reaction products generated in greater amounts are the same as in Example 17. FIG. 1 shows a chromatogram with products distribution and retention time.

Example 22. Thermal Assessment at 290° C. of Lignin Kraft with Water/Ethanol Ratio (50/50), 1 Hour

The thermal assessment was carried out at 290° C. in a batch-type reactor (Reactor Parr 4842) with a 250 mL capacity. The water/ethanol ratio (v/v) was 50/50. 2 g of lignin Kraft was used in the reaction test under a 4,137 kPa (600 psi) hydrogen pressure with mechanical stirring at 1000 rpm. Once said conditions were reached the reaction is left for a period of 1 hour. When the reaction is completed, the reactor is dissembled from the heating system to be cooled immediately. The reaction product was treated under the same methodology used in Example 14. The lignin conversion was of 57% by weight with a reaction time of 1 hour. The reaction products generated in greater amounts are the same as in Example 17. FIG. 1 shows a chromatogram with products distribution and retention time.

Example 23. Thermal Assessment at 290° C. of Lignin Kraft with Water/Ethanol Ratio (50/50), 6 Hours

The thermal assessment was carried out at 290° C. in a batch-type reactor (Reactor Parr 4842) with a 250 mL capacity. The water/ethanol ratio (v/v) was 50/50. 2 g of lignin Kraft was used in the reaction test under a 4,137 kPa (600 psi) hydrogen pressure with mechanical stirring at 1000 rpm. Once said conditions were reached the reaction is left for a period of 6 hours. When the reaction is completed, the reactor is dissembled from the heating system to be cooled immediately. The reaction product was treated under the same methodology used in Example 14. The lignin conversion was of 57% by weight with a reaction time of 6 hours. The reaction products generated in greater amounts are the same as in Example 17. FIG. 1 shows a chromatogram with products distribution and retention time.

Example 24. Thermal Assessment at 290° C. of Lignin Kraft with Water/Ethanol Ratio (50/50), in Basic Medium

Conversion of lignin based on the reaction medium. The thermal assessment was carried out at 290° C. in a batch-type reactor (Reactor Parr 4842) with a 250 mL capacity. The water/ethanol ratio (v/v) was 60/50. Three hundred mg of NaOH was used as basic medium. 2 g of lignin Kfraft was used in the reaction test under a 4,137 kPa (600 psi) hydrogen pressure with mechanical stirring at 1000 rpm. Once said conditions were reached the reaction is left for a period of 3 hours. When the reaction is completed, the reactor is dissembled from the heating system to be cooled immediately. The reaction product was treated under the same methodology used in Example 14. The lignin conversion was of 51.3% by weight in basic medium. The reaction products generated in greater amounts are the same as in Example 17. FIG. 1 shows a chromatogram with products distribution and retention time.

TABLE 2 Thermal assessments with lignin Kraft. Temperature Ethanol:H₂O Conversion Time Selectivity (%) (° C.) ratio (v/v) (% weight) (h) Aromatic Non-aromatic Example # 60 50:50 0.50 3 100.00 0.00 14 80 50:50 3.80 3 100.00 0.00 15 140 50:50 11.5 3 95.08 4.92 16 220 50:50 39.7 3 98.42 1.42 17 260 50:50 53.4 3 60.21 39.79 18 290 50:50 59.0 3 55.30 44.70 19 290 80:20 48.0 3 56.54 43.46 20 290 20:80 58.0 3 37.87 62.13 21 290 20:80 57.0 1 51.50 48.50 22 290 50:50 67.0 6 78.90 20.18 23 290 50:50 51.3 3 (1) 50.98 49.01 24 290 50:50 69.0 3 (2) 31.53 68.47 25 (1) Basic medium (NaOH); (2) Acid medium (HCl).

Example 25. Thermal Assessment at 290° C. of Lignin Kraft with Water/Ethanol Ratio (50/50), in Acid Medium

Conversion of lignin based on the reaction medium. The thermal assessment was carried out at 290° C. in a batch-type reactor (Reactor Parr 4842) with a 250 mL capacity. The water/ethanol ratio (v/v) was 50/50. For the acid medium, 300 mg of HCl was used. Two g of lignin Kfraft was used in the reaction test under a 4,137 kPa (600 psi) hydrogen pressure with mechanical stirring at 1000 rpm. Once said conditions were reached the reaction is left for a period of 3 hours. When the reaction is completed, the reactor is dissembled from the heating system to be cooled immediately. The reaction product was treated under the same methodology used in Example 14. The lignin conversion was of 69% by weight in acid medium; the reaction products generated in greater amounts are the same as in Example 17. FIG. 1 shows a chromatogram with products distribution and retention time.

Example 26. Thermal Assessment of Sugar Cane Bagasse Lignin (SCBL) at 260° C.

The thermal assessment was carried out at 260° C. batch-type reactor (Reactor Parr 4842) with a 300 mL capacity. The water/ethanol ratio (v/v) was of 50/50. 10 g sugar cane bagasse lignin (SCBL) were used in a reaction test under an 7102 kPa (1030 psi) nitrogen pressure with mechanical stirring of 250 rpm. Once said conditions were reached, the reaction is left for a period of 1 hour. When the reaction was completed, the reactor is dissembled from the heating system to be cooled immediately. The reaction product was treated under the same methodology used in Example 14. The sugar cane bagasse lignin conversion was ≥90% mass base, wherein the selectivity was of 67.3% to aromatic products, 12.3% to furans and 20.4% to non-aromatic compounds.

Example 27. Assessment of the EAS Catalytic Formulation with Sugar Cane Bagasse Lignin (SCBL)

The catalytic assessment with the EAS catalyst prepared as set forth under Example 2, was carried out at 260° C. in a batch-like reactor (Reactor Parr 4842) with a 300 mL capacity. The water/ethanol ratio (v/v) was of 50/50. 10 g sugar cane bagasse lignin (SCBL) were used in a reaction test, the pressure was kept at 7102 kPa (1030 psi) nitrogen pressure with mechanical stirring of 250 rpm and 1 g of the EAS catalyst. Once said conditions were reached, the reaction is left for a period of 1 hour. When the reaction was completed, the reactor is dissembled from the heating system to be cooled immediately. The reaction product was treated under the same methodology used in Example 14. The IMP lignin conversion was ≥90% mass base, the selectivity was of 62.8% to aromatic products, 4.7% to furans and 32.4% to non-aromatic compounds.

Example 28. Assessment of the 15Ni-EAS Catalytic Formulation with Sugar Cane Bagasse Lignin (SCBL)

The thermal assessment was carried out at 260° C. in a batch-like reactor (Reactor Parr 4842) with a 300 mL capacity. The water/ethanol ratio (v/v) was of 50/50. 10 g sugar cane bagasse lignin (SCBL) were used in the reaction test under a 7102 kPa (1030 psi) nitrogen pressure with mechanical stirring of 250 rpm and 1 g of the 15Ni-EAS catalyst prepared according to the methodology described under Example 8. Once said conditions were reached, the reaction is left for a period of 1 hour. When the reaction was completed, the reactor is dissembled from the heating system to be cooled immediately. The reaction product was treated under the same methodology used in Example 17. The lignin IMP conversion was ≥90% mass base, the selectivity was of 49.6% to aromatic products, 6.2% to furans and 44.2% to non-aromatic compounds.

Example 29. Assessment of the MMZ-112C Catalytic Formulation with Sugar Cane Bagasse Lignin (SCBL)

The thermal assessment was carried out at 260° C. in a batch-like reactor (Reactor Parr 4842) with a 300 mL capacity. The water/ethanol ratio (v/v) was of 50/50. 10 g sugar cane bagasse lignin (SCBL) were used in the reaction test under a 7102 kPa (1030 psi) nitrogen pressure with mechanical stirring of 250 rpm and 1 g of the MMZ-112C catalyst prepared according to the methodology described under Example 4. Once said conditions were reached, the reaction is left for a period of 1 hour. When the reaction was completed, the reactor is dissembled from the heating system to be cooled immediately. The reaction product was treated under the same methodology used in Example 8. The sugar cane bagasse lignin conversion was ≥90% mass base, wherein the selectivity was of 67.6% to aromatic products, 6.1% to furans and 26.3% to non-aromatic compounds.

Example 30. Assessment of the CMA Catalytic Formulation with Sugar Cane Bagasse Lignin (SCBL)

The thermal assessment was carried out at 260° C. in a batch-like reactor (Reactor Parr 4842) with a 300 mL capacity. The water/ethanol ratio (v/v) was of 50/50. 10 g sugar cane bagasse lignin (SCBL) were used in the reaction test under a 7102 kPa (1030 psi) nitrogen pressure with mechanical stirring of 250 rpm and 1 g of the CMA catalyst (commercial reference catalyst alumina based) Table 1. Once said conditions were reached, the reaction is left for a period of 1 hour. When the reaction was completed, the reactor is dissembled from the heating system to be cooled immediately. The reaction product was treated under the same methodology used in Example 14. The sugar cane bagasse lignin (SCBL) conversion was ≥90% mass base, wherein the selectivity was of 47.64% to aromatic products, 5.3% to furans and 44.7% to non-aromatic compounds.

Example 31. Thermal Assessment with Sugar Cane Bagasse (SCB) at 260° C. at 7102 kPa (1030 psi)

The thermal assessment was carried out at 260° C. in a batch-like reactor (Reactor Parr 4842) with a 300 mL capacity. The water/ethanol ratio (v/v) was of 50/50. Twenty g sugar cane bagasse (SCB) were used in the reaction test under a 7102 kPa (1030 psi) nitrogen pressure with mechanical stirring of 250 rpm. Once said conditions were reached, the reaction is left for a period of 1 hour. When the reaction was completed, the reactor is dissembled from the heating system to be cooled immediately. The reaction product was treated under the same methodology used in Example 14. The sugar cane bagasse (SCB) conversion was ≥90% mass base, wherein the selectivity was of 39.1% to aromatic products, 13.9% to furans and 47.1% to non-aromatic compounds.

Example 32. Thermal Assessment with Sugar Cane Bagasse (SCB) at 260° C. at 12,410 kPa (1800 psi)

The thermal assessment was carried out at 260° C. in a batch-like reactor (Reactor Parr 4842) with a 300 mL capacity. The water/ethanol ratio (v/v) was of 60/50. 20 g sugar cane bagasse (SCB) were used in the reaction test under a 12,410 kPa (1800 psi) nitrogen pressure with mechanical stirring of 250 rpm. Once said conditions were reached, the reaction is left for a period of 1 hour. When the reaction was completed, the reactor is dissembled from the heating system to be cooled immediately. The reaction product was treated under the same methodology used in Example 14. The sugar cane bagasse (SCB) conversion was ≥90% mass base, wherein the selectivity was of 57.7% to aromatic products, 19.8% to furans and 23.4% to non-aromatic compounds.

Example 33. Assessment of the 15Ni-EASMeso Catalytic Formulation from Sugar Cane Bagasse (SCB)

The thermal assessment was carried out at 260° C. in a batch-like reactor (Reactor Parr 4842) with a 300 mL capacity. The water/ethanol ratio (v/v) was of 50/50. 20 g sugar cane bagasse were used in the reaction test under a 7102 kPa (1030 psi) nitrogen pressure with mechanical stirring of 250 rpm and 1 g of the 15Ni-EASMeso catalyst prepared according to the methodology described under Example 10. Once said conditions were reached, the reaction is left for a period of 1 hour. When the reaction was completed, the reactor is dissembled from the heating system to be cooled immediately. The reaction product was treated under the same methodology used in Example 14. The sugar cane bagasse conversion was ≥90% mass base, wherein the selectivity was of 37.3% to aromatic products, 22% to furans and 40.6% to non-aromatic compounds.

TABLE 3 Assessments with SCBL y SCB. Selectivity (%) Weight Pressure Non- Catalyst Lignin (g) (kPa) Aromatic Furans aromatic Example # Thermal LBC 10 7102 67.3 12.3 20.4 26 EAS LBC 10 7102 62.8 4.7 32.4 27 15Ni-EAS LBC 10 7102 49.6 6.2 44.2 28 MMZ-112C LBC 10 7102 67.6 6.1 26.3 29 CMA LBC 10 7102 47.64 5.3 44.7 30 Thermal BC 20 7102 39.1 13.9 47.1 31 Thermal BC 20 7102 57.7 19.8 23.4 32 15Ni-EASMeso BC 20 7102 37.3 22 40.6 33 MMZ-112C BC 20 7102 52.7 27 20.3 34 Conversion: ≥90% by weight; Temperature: 260° C.; Ethanol:H₂O ratio (v/v): 60:50; Catalyst's weight: 1 g; SCBL: Sugar cane bagasse lignin; SCB: Sugar cane bagasse.

Example 34. Assessment of the MMZ-112C Catalytic Formulation from Sugar Cane Bagasse (SCB)

The thermal assessment was carried out at 260° C. in a batch-like reactor (Reactor Parr 4842) with a 300 mL capacity. The water/ethanol ratio (v/v) was of 50/50. 20 g sugar cane bagasse were used in the reaction test under a 7102 kPa (1030 psi) nitrogen pressure with mechanical stirring of 250 rpm and 1 g of the MMZ-112C catalyst prepared according to the methodology described under Example 4. Once said conditions were reached, the reaction is left for a period of 1 hour. When the reaction was completed, the reactor is dissembled from the heating system to be cooled immediately. The reaction product was treated under the same methodology used in Example 14. The sugar cane bagasse conversion was ≥90% mass base, wherein the selectivity was of 52.7% to aromatic products, 27% to furans and 20.3% to non-aromatic compounds.

Examples 35, 36 and 37. Assessment in Sodium Lignosulfonate Depolymerisation in a Pilot Micro-Plant with 15Ni-EAS Catalyst

A sodium lignosulfonate depolymerisation catalytic assessment was carried out in a pilot micro-plant system equipped with a fixed bed tubular reactor operating in ascending flow. 7.5 mL of granulated catalyst (15Ni-EAS, mesh EE.UU.16-20, about 1 mm average particle size, prepared according to the methodology described under Example 8) were loaded diluted with an equivalent volume of SiC EE.UU. mesh 60 (about 0.25 mm diameter). Before the assays, the catalyst was subjected to a reduction process consisting in passing H₂ flow (5 L/h), at 70 kg/cm² and 350° C. Once the catalyst was active (1 hour) the system was taken to the lignin depolymerisation assessment conditions (N₂ flow of 5 L/h, 70 kg/cm² and T=260° C.) feeding sodium lignosulfonate (2 g in 100 mL ethanol/water mixture, 50/50 vol/vol) at a speed such that allows carrying out the assessment at LHSV 5, 3, and 2 h⁻¹. The liquid products obtained from the reaction showed a transparent yellow colour. The liquid products obtained from the reaction showed a transparent yellow colour. The separation of the organic fraction was carried out by adding dichloromethane following the same procedure as described under Example 8. The aqueous fraction resulted totally transparent, indicating the absence of dissolved lignin therein and that the depolymerisation was of 100%. The product selectivity results were grouped as oxygenated and deoxygenated aromatic, paraffin, olefin, isoparaffin and naphthenes, alcohols and ketones, and ethers and esters. The results are shown in Table 4, and it can be appreciated that an LHSV at 3 h⁻¹ the selectivity of aromatic hydrocarbons was of 52% of which 26% correspond to deoxygenated aromatic and the 26% leftover corresponds to oxygenated aromatic, which indicates that the catalyst 15Ni-EAS carries out the deoxygenation of the oxygenated aromatics produced during lignin depolymerisation. Moreover, a noticeable selectivity to paraffin and isoparaffin, olefin and naphthenes is observed, indicating that an opening of the aromatic rings is carried out. The results of the products selectivity are shown in Table 4.

TABLE 4 Sodium lignosulfonate depolymerisation with 15Ni-EAS catalyst. Effect of LHSV (liquid hourly space velocity). Selectivity (%) LHSV Arom. no Arom. (h⁻¹) oxi. oxi. Alcohols Hisopara. Paraffin Naphthenes Others No id. Example. 5 6.53 28.84 3.70 2.46 22.10 0.24 3.79 32.34 35 3 26.00 26.00 1.26 2.98 9.81 2.24 9.8 21.91 36 2 25.80 4.42 0.0 6.50 16.57 0.46 1.73 44.52 37 Temperature: 260° C.; Ethanol:H₂O ratio (v/v) 50:50; Catalyst volume: 7.5 ml; N₂ Pressure: 70 Kg/cm².

Examples 38, 39 and 40. Assessment in Sodium Lignosulfonate Depolymerisation in a Pilot Micro-Plant with 15Co-EAS Catalyst

A sodium lignosulfonate (pre-treated) depolymerisation catalytic assessment was carried out in a pilot micro-plant system equipped with a fixed bed tubular reactor operating in ascending flow. 7.5 mL of granulated catalyst (15Co-EAS, prepared according to the methodology described under Example 9, mesh EE.UU.16-20, about 1 mm average particle size). Before the activity assessment assays, the catalyst material was reduced in H₂ flow (5 L/h), at 70 kg/cm² and 350° C. Once the catalyst was active (1 hour) the system was taken to the lignin depolymerisation assessment conditions (N₂ flow of 5 L/h, 70 kg/cm² and T=260° C.) feeding pre-treated sodium lignosulfonate (2 g in 100 mL ethanol/water mixture, 50/50 vol/vol). During pre-treatment, a mixture of 6 g lignin+150 mL H₂O+150 mL ethanol was subjected for 1 hour at 260° C., an initial pressure of N₂ at 70 kg/cm₂. Speed spaces were used in the interval of 2 to 5 h⁻¹. The product selectivity results are shown in Table 5.

TABLE 5 Sodium lignosulfonate depolymerisation with 15Co-EAS catalyst. Effect of LHSV. Selectivity (%) Olef.- LHSV Arom. Arom. Isoparaf.- Ether- Naphthenes- (h⁻¹) no oxi. oxi. Alcohols Paraffin Ester furans Others No id. Example 5 12.86 38.61 12.04 5.40 4.27 1.87 0.09 24.86 38 3 0.59 56.30 15.97 1.46 0.38 3.24 0.02 22.04 39 2 5.21 39.50 14.29 11.96 2.42 3.39 3.07 20.16 40 Temperature: 260° C.; Ethanol:H₂O ratio (v/v) 50:50; Catalyst volume: 7.5 ml; N₂ Pressure: 70 Kg/cm².

Examples 41, 42 and 43. Assessment in Sodium Lignosulfonate Depolymerisation in a Pilot Micro-Plant with EAS Catalyst

A sodium lignosulfonate (pre-treated) depolymerisation catalytic assessment was carried out in a pilot micro-plant system equipped with a fixed bed tubular reactor operating in ascending flow. 7.5 mL of the catalyst prepared according to the methodology described under Example 2, granulated (EAS, mesh EE.UU.16-20, about 1 mm average particle size) were loaded. Before the activity assessment assays, the catalytic material was reduced in H₂ flow (5 L/h), at 70 kg/cm² and 350° C. Once the catalyst was active (1 hour) the system was taken to the lignin depolymerisation assessment conditions (N₂ flow of 5 L/h, 70 kg/cm² and T=260° C.) feeding sodium lignosulfonate (pre-treated) (2 g in 100 mL ethanol/water mixture, 50/50 vol/vol). During the pre-treatment, a mixture of 6 g lignin+150 mL H₂O+150 ethanol was subjected for 1 hour at 260° C., at N₂ initial pressure of 70 kg/cm².

Speed spaces in the interval of 2 to 5 h⁻¹ were used. The results of the aromatic products selectivity are shown in Table 6.

Examples 44, 45 and 46. Assessment in Sugar Cane Bagasse (SCB) Lignin Depolymerisation in Pilot Micro-Plant

A sugar cane bagasse lignin thermal depolymerisation assessment was carried out in a pilot micro-plant system equipped with a fixed bed tubular reactor operating in ascending flow. 7.5 mL of the granulated catalyst (15Ni-EAS prepared according to the methodology described under Example 8, mesh EE.UU.16-20, about 1 mm average particle size) were loaded. Before the activity assessment assays, the catalytic material was reduced in H₂ flow (5 L/h), at 70 kg/cm² and 350° C. Once the catalyst was active (1 hour) the system was taken to the lignin depolymerisation assessment conditions (N₂ flow of 5 L/h, 70 kg/cm² and T=260° C.) feeding pre-treated sugar cane bagasse lignin (3.3 g in 100 mL ethanol/water mixture, 50/50 vol/vol). During the pre-treatment, a mixture of 10 g lignin+150 mL H₂O+150 ethanol was subjected for 1 hour at 260° C., at N₂ initial pressure of 70 kg/cm².

Speed spaces in the interval of 2 to 5 h⁻¹ were used. The results of the aromatic products selectivity are shown in Table 7.

TABLE 6 Catalytic assessment of sodium lignosulfonate with EAS catalyst. Effect of LHSV. Selectivity (%) Olef.- LHSV Arom. Arom. Isoparaf.- Ether- Naphthenes- (h⁻¹) no oxi. oxi. Alcohols Paraffin Ester furans Others No id. Example 5 1.08 40.83 7.33 0 2.35 3.05 0.72 44.64 41 3 1.08 40.70 7.64 0 2.35 2.88 0.71 44.64 42 2 2.45 56.38 17.34 0 0.95 4.79 0.01 18.08 43 Temperature: 260° C.; Ethanol:H₂O ratio (v/v) 50:50; Catalyst volume: 7.5 ml; N₂ Pressure: 70 Kg/cm².

Examples 47, 48, 49 and 50. Assessment of Depolymerisation of Black Liqueur Lignin from Paper Industry in Pilot Micro-Plant

A depolymerisation catalytic assessment was carried out with black liqueur lignin, a paper industry residue, in a pilot micro-plant system with a fixed bed tubular reactor operating in ascending flow. 7.5 mL of SiC EE.UU. mesh 60 (about 0.25 mm diameter) were loaded. The system was taken to lignin depolymerisation assessment conditions (N₂ flow of 5 L/h, 70 kg/cm² and T=260° C.) feeding black liqueur lignin (3.33 g in 100 mL ethanol/water mixture, 50/50 vol/vol). Speed spaces in the interval of 2 to 5 h⁻¹ were used. The results of the aromatic products selectivity are shown in Table 8.

TABLE 7 Assessment of sugar cane bagasse lignin (SCBL) depolymerisation with 15Ni- EAS catalyst. Effect of LHSV. Selectivity (%) Olef- LHSV Arom. Arom. Isoparaf.- Ether- Naphthenes- (h⁻¹) no oxi. oxi. Alcohols Paraffin Ester furans Others No id. Example. 5 0.38 48.17 1.34 0.92 10.30 10.33 1.82 26.74 44 3 18.16 41.05 5.79 2.04 3.42 7.60 0.94 21.00 45 2 3.43 61.65 1.97 0 2.43 14.97 0.98 14.57 46 Temperature: 260° C.; Ethanol:H₂O ratio (v/v) 50:50; Catalyst volume: 7.5 ml; N₂ Pressure 70 Kg/cm².

Examples 51, 52 and 53. Catalytic Assessment of Sodium Lignosulfonate Depolymerisation in Pilot Micro-Plant at Different Hydrogen Pressures

A catalytic assessment of (pre-treated) sodium lignosulfonate depolymerisation was carried out in a pilot micro-plant system equipped with a fixed bed tubular reactor in ascending flow. 7.5 mL of SiC EE.UU. mesh 60 (about 0.25 mm diameter) were loaded at the bottom of the reactor, and then an equivalent volume of granulated catalyst (15Ni-EAS prepared according to the methodology under Example 8, mesh EE.UU. 16-20, about 1 mm average particle size) was added. Before the activity assessment assays, the catalytic material was reduced in H₂ flow (5 L/h), at 70 kg/cm² and 350° C. Once the catalyst was active (1 hour) the system was taken to the lignin depolymerisation assessment conditions (N₂ flow of 5 L/h, 70 kg/cm² and T=260° C.) feeding pre-treated sodium lignosulfonate lignin (2 g in 100 mL ethanol/water mixture, 50/50 vol/vol). During the pre-treatment, a mixture of 6 g lignin+150 mL H₂O+150 ethanol was subjected for 1 hour at 260° C., at N₂ initial pressure of 70 kg/cm². The hydrogen partial pressure effect was studied in the interval of 30 to 70 Kg/cm². The results of the aromatic products selectivity are shown in Table 9.

TABLE 8 Thermal assessment of black liqueur lignin from paper industry. Effect of LHSV. Selectivity (%) Olef.- LHSV Arom. Arom. Isoparaf.- Ether- Naphthenes- (h⁻¹) no oxi oxi. Alcohols Paraffin Ester furans Nitrog. No id. Example. 5 36.2 44.57 0.92 12.09 0 1.75 0 4.47 47 3 5.05 86.19 1.06 3.67 0 0 0 4.03 48 2 0 91.46 1.12 0 0 2.96 0 4.45 49 1 0 92.45 0 0 0 0 3 4.54 50 Temperature: 260° C.; Ethanol:H₂O ratio (v/v) 50:50; SiC volume: 7.5 ml; N₂ Pressure: 70 Kg/cm²

TABLE 9 Assessment of pre-treated sodium lignosulfonate depolymerisation with 15Ni- EAS catalyst. Effect of H₂ Pressure Selectivity (%) P Arom. Arom. (Kg/cm²) no oxi. oxi. Alcohols Isoparaf. Paraffin Naphthenes Others No id. Example. 30 0 67.53 13.73 0 7.33 1.06 4.96 5.39 51 50 0 71.00 13.76 0 3.99 0 2.2 9.05 52 70 0 70.08 17.42 0 5.79 0 0 6.71 53 Temperature: 260° C.; Ethanol:H₂O ratio (v/v) 50:50; Catalyst volume: 7.5 ml; LHSV: 3 h⁻¹. 

1. A process of lignin depolymerisation and deoxygenation for obtaining aromatic compounds, the process comprising: dissolving a lignin in a protic liquid, creating a dissolved protic lignin mixture; reacting the dissolved protic lignin mixture in one of a batch reaction system or a continuous flow reaction system at either an inert or reducing atmosphere; wherein the reaction is carried out at a determined reaction temperature of between 40° C. to 320° C., inclusive, and a determined operation pressure of from 5 kg/cm² to 100 kg/cm², inclusive.
 2. The process according to claim 1, wherein reacting the dissolved protic lignin mixture in the batch reaction system produces a plurality of oxygenated aromatic hydrocarbons by thermal and catalytic depolymerisation.
 3. The process according to claim 1, wherein reacting the dissolved protic lignin mixture in the continuous flow system produces a plurality of deoxygenated aromatic hydrocarbons.
 4. The process according to claim 1, wherein the lignin is black liqueur lignin.
 5. The process according to claim 1, wherein the dissolving a lignin comprises dissolving the lignin in a mixture of protic solvents placed in a container, creating a dissolved protic lignin mixture, and sealing the container; and wherein the reacting the dissolved protic lignin mixture comprises heating the dissolved protic lignin mixture at the determined reaction temperature, stirring the dissolved protic lignin mixture, and applying pressure with one of either an inert gas or hydrogen pressure to the reaction to maintain a set of determined reaction conditions for a determined reaction time.
 6. The process according to claim 2, wherein the reaction is carried out thermally and without a catalyst.
 7. The process according to claim 5, wherein the mixture of selected protic solvents is a mixture of an alcohol and water.
 8. The process according to claim 7, wherein the alcohol is selected from a group consisting of methanol, ethanol, 1-propanol, 1-butanol, and 2-butanol.
 9. The process according to claim 5, wherein the mixture of protic solvents comprises a mixture of alcohol water in a ratio of either 30% to 70% or 70% to 30% v/v.
 10. The process according to claim 5, wherein the determined reaction temperature is between 100° C. and 280° C., inclusive.
 11. The process according to claim 5, wherein the determined operation pressure is between 10 kg/cm² and 80 kg/cm², inclusive.
 12. The process according to claim 5, wherein the applying pressure comprises adding an inert gas selected from the group consisting of helium, argon, and nitrogen to reach the determined operation pressure.
 13. The process according to claim 2, wherein the determined operation pressure is reached by adding a reducing gas to the dissolved protic lignin mixture, the reducing gas comprising either pure hydrogen or hydrogen diluted with an inert gas.
 14. The process according to claim 5, wherein the determined reaction time is between 0.5 hours and 4 hours, inclusive.
 15. The process according to claim 5, wherein the stirring the dissolved protic lignin mixture further comprises mechanically stirring the dissolved protic lignin mixture at a speed between 200 rpm and 1200 rpm.
 16. The process according to claim 2, wherein the lignin is soluble in the protic liquid.
 17. The process according to claim 5, wherein the lignin is selected from a group containing sodium lignosulfonate, lignin Kraft, organosolv lignin, lignin obtained from lignocellulosic residues after the enzymatic hydrolysis of cellulose, lignin obtained directly from lignocellulosic residues, and black liqueur.
 18. The process according to claim 5, wherein the dissolved protic lignin mixture comprises a ratio of lignin to protic solvent of between 1 g/L to 100 g/L.
 19. The process according to claim 2, wherein the lignin is insoluble in the protic liquid, and the reaction further comprises solubilizing the lignin during a depolymerisation reaction.
 20. The process according to claim 5, wherein the lignin comprises one of either a lignocellulosic residue or a biomass.
 21. The process according to claim 20, wherein the lignocellulosic residue or biomass is selected from a group consisting of sugar cane bagasse, wood chip, and a lignocellulosic residue with a lignin content greater than 15% by weight.
 22. The process according to claim 5, further comprising separating a collection of depolymerised organic products by adding an aprotic polar solvent to the dissolved protic lignin mixture.
 23. The process according to claim 22, wherein the aprotic polar solvent used is selected from a group containing tetrahydrofuran, dichloromethane and acetone.
 24. The process according to claim 22, further comprising separating the depolymerised organic products from the aprotic polar solvent by evaporation at the solvent's boiling temperature, the boiling temperature being between 30° C. and 80° C., inclusive, to obtain a collection of obtained products.
 25. The process according to claim 24, wherein the obtained products consist of phenolic oxygenated aromatic hydrocarbons, the phenolic oxygenated hydrocarbons having a set of identified peaks with an area of between 30% and 100% when analyzed by a gas chromatography system coupled to a mass spectrometer.
 26. The process according to claim 5, further comprising separating a collection of depolymerised products from the mixture, wherein the depolymerised products have a set of identified peaks with an area of between 30% and 90%, inclusive, when analyzed by a gas chromatography system equipped with a mass spectrometer.
 27. The process according to claim 3, further comprising passing a continuous flow of lignin dissolved in a protic solvent mixed with one of an inert gas, a reducing gas, or a mixture of an inert gas and a reducing gas through a tubular reactor packed with one of a catalyst, an inert material, or a mixture of a catalyst and an inert material at a determined spatial time LHSV, pressure and temperature, resulting in a dissolved lignin protic product.
 28. The process according to claim 27, further comprising passing the dissolved lignin protic product through a cationic exchange resin, and subsequently passing the dissolved lignin protic product through an anionic exchange resin in order to eliminate impurities, the impurities including a group of inorganic cations including Na, K and La and or a group of ions including SO₄ ⁻ and Cl.
 29. The process according to claim 3, wherein the lignin is selected from a group consisting of sodium lignosulfonate, lignin Kraft, sugar cane bagasse lignin and black liqueur.
 30. The process according to claim 3, wherein the reaction is carried out at inert atmosphere using an inert gas selected from a group consisting of nitrogen, helium and argon.
 31. The process according to claim 3, wherein the reaction is carried out thermally and without a catalyst, and wherein the reaction system is packed with an inert material selected from a group consisting of quartz, alpha alumina and silicon carbide.
 32. The process according to claim 3, wherein the reaction is carried out in the presence of a catalyst.
 33. The process according to claim 3, wherein the reaction is carried out at a reducing atmosphere with one of hydrogen or a mixture of hydrogen with inert gas.
 34. The process according to claim 3, wherein the reaction is carried out at an inert atmosphere, and wherein said determined operation pressure is between 30 kg/cm² to 80 kg/cm², inclusive.
 35. The process according to claim 3, wherein the reaction is carried out at a hydrogen reducing atmosphere, and wherein the determined operation pressure is between 5 kg/cm² to 70 kg/cm², inclusive.
 36. The process according to claim 3, wherein the determined reaction temperature is between 100° C. and 320° C., inclusive.
 37. The process according to claim 3, wherein the reaction is carried out with a determined spatial time LHSV, the determined spatial time LHSV is between 0.5 h⁻¹ to 10 h⁻¹, inclusive.
 38. The process according to claim 3, wherein the reaction is thermally developed obtaining a collection of oxygenated aromatic hydrocarbons, the collection of oxygenated aromatic hydrocarbons having a selectivity between 40% and 80%, inclusive.
 39. The process according to claim 3, wherein the process of lignin depolymerisation and deoxygenation occurs with a collection of oxygenated aromatic compounds and deoxygenated aromatic compounds in the presence of a catalyst.
 40. The process according to claim 39, wherein the deoxygenated aromatic compounds have a selectivity of between 25% to 70%, inclusive.
 41. The process according to claim 3, wherein the deoxygenated aromatic hydrocarbons are obtained from a single stage from a collection of renewable raw materials.
 42. The process according to claim 39, wherein the oxygenated and deoxygenated aromatic compounds have a selectivity of between 30% and 100%, inclusive.
 43. A catalytic composition used in a process of lignin depolymerisation and deoxygenation for obtaining aromatic hydrocarbons according to claims 5 and 27, the process comprising: dissolving a lignin in a mixture of protic solvents placed in a container, creating a dissolved protic lignin mixture, and sealing the container; reacting the dissolved protic lignin mixture in one of a batch reaction system or a continuous flow reaction system at either an inert or reducing atmosphere; stirring the dissolved protic lignin mixture; applying pressure with one of either an inert gas or hydrogen pressure to the reaction to maintain a set of determined reaction conditions for a determined reaction time; and wherein the reaction is carried out at a determined reaction temperature of between 40° C. to 320° C., inclusive, and a determined operation pressure of from 5 kg/cm² to 100 kg/cm², inclusive; wherein the catalytic composition comprises a non-noble element of Group VIIIB of the periodic table, the non-noble element supported in a support material, the support material comprising one of either an inorganic oxide or a mixture of a surface modified inorganic oxides with a second inorganic oxide.
 44. The catalytic composition according to claim 43, wherein the non-noble element from Group VIIIB of the periodic table is selected from a group consisting of Fe, Co, and Ni.
 45. The catalytic composition according to claim 43, wherein the support material comprises an inorganic oxide with a specific high area, the inorganic oxide with specific high area selected from a group consisting of alumina, silica, titania, zirconia and a mixture of alumina, silica, titania, and zirconia.
 46. The catalytic composition according to claim 43, wherein the support material comprises an inorganic oxide, the inorganic oxide surface modified with a separate inorganic element.
 47. The catalytic composition according to claim 43, wherein the support material comprises one of either an inorganic oxide or a mixture of inorganic oxides with a mesoporous structure.
 48. The catalytic composition according to claim 43, wherein the support material comprises an inorganic oxide, the inorganic oxide selected from a mesoporous alumina modified by a second inorganic oxide, the second inorganic oxide selected from silicon dioxide to weaken the metal-support interaction, and wherein the material is mixed with a third silico aluminate component with a mesoporous zeolitic structure.
 49. The catalytic composition according to claim 43, wherein the support material has an area between 200 m²/g and 500 m²/g, inclusive, an average pore diameter from 8 nm to 30 nm, inclusive, and pore volume from 0.5 cc/g to 2.0 cc/g, inclusive.
 50. The catalytic composition according to claim 43, wherein the support material is prepared by selecting an aluminum oxyhydroxide in bohemite phase; peptizing the aluminum oxyhydroxide with an inorganic acid at a determined concentration, the determined concentration between 0.05 M and 2 M, inclusive, for a time period of between 2 hours to 12 hours, inclusive, at a temperature of between 50° C. and 80° C., inclusive; cooling at a predetermined room temperature and adding a high volume surfactant, creating a suspension; stirring the suspension for a time period between 4 hours to 24 hours, inclusive; drying the suspension for a first drying period, the first drying period including a temperature of 50° C. for a time period between 12 hours to 24 hours, inclusive, and drying the suspension for a second drying period, the second drying period including a temperature of between 80° C. to 90° C., inclusive, for a time period between 12 hours to 24 hours, inclusive, creating a resulting solid material; burning the resulting solid material in an air flow to remove a surfactant in the resulting solid material, passing at a flow from 100 mL/min to 150 mL/min with a heating speed of 0.8° C./min until reaching a first reaction temperature of 300° C., the first reaction temperature maintained for a time period of between 4 hours to 8 hours, inclusive, and increasing the material to a second reaction temperature of between 500° C. and 600° C., the second reaction temperature maintained for a time period of between 4 hours to 12 hours, inclusive, creating a burnt material; creating a separate solution, said separate solution comprising a mixture of anhydrous ethanol with tetra-ethyl-orthosilicate stirred for a time period of between 0.5 hours to 2 hours, inclusive, at a temperature of between 50° C. and 80° C., inclusive; cooling the solution at a predetermined room temperature and carrying out hydrolysis by drop-wise addition of a mixture comprising an ethanol solution, double-distilled water and an inorganic acid, and stirring the solution for a time period of between 0.5 hours to 1 hour, inclusive; adding the burnt material to said stirred solution and allowing the mixture of the burnt material and the stirred solution to stand for a time period of 6 hours to 18 hours, resulting in a suspension; filtering the suspension to recover a solid present in the suspension, creating a filtered product; drying the filtered product at a temperature of between 100° C. and 120° C., inclusive, and burning the filtered product in an air flow of between 100 mL/min and 150 mL/min, inclusive, at a temperature of between 400° C. and 600° C., inclusive, for a time period of 2 hours to 12 hours, inclusive.
 51. The catalytic composition according to claim 43, wherein the support material is formulated in a cylindrical or trilobal extrudes by mixing the support material with aluminum oxyhydroxide in bohemite phase; adding a solution, the solution comprising either an inorganic or an organic acid at a concentration of between 0.5 to 5% by weight, creating a resulting mixture; mashing the resulting mixture to obtain a paste with rheology to be extruded; extruding the paste using Minibonot equipment with cylindrical, trilobal and tetralobular output, creating a resulting material; drying the resulting material at a room temperature for a time period of 12 hours to 24 hours, inclusive, creating a semi-dried material; drying the semi-dried material at a temperature between 100° C. to 120° C., inclusive, for a time period of 6 hours to 12 hours, inclusive; and burning at a temperature of between 400° C. and 600° C., inclusive, for a time period of between 4 hours to 12 hours, inclusive.
 52. The catalytic composition according to claim 43, wherein the composition consists of non-modified mesoporous alumina mixed with an aluminum oxyhydroxide in bohemite phase.
 53. The catalytic composition according to claim 43, wherein the support material is modified with a second inorganic oxide.
 54. The catalytic composition according to claim 47, wherein the support material comprises between 10% to 70%, inclusive, mesoporous alumina, 10% to 70%, inclusive, mesoporous zeolite, and 10% to 70%, inclusive, aluminum oxyhydroxide in bohemite phase.
 55. The catalytic composition according to claim 48, wherein the support material comprises between 30% to 70%, inclusive, mesoporous alumina and 30% to 70%, inclusive, aluminum oxyhydroxide in bohemite phase.
 56. The catalytic composition according to claim 43, wherein the non-noble element from Group VIIIB of the periodic table is integrated into the support material by solubilizing a precursor salt containing the non-noble element from Group VIIIB of the periodic table in a protic liquid, selecting one of either alcohol or water; concentrating a volume to be absorbed into the pores of the support material, creating a solution; contacting the solution with the extruded support material, creating a resulting product; leaving the resulting product standing for a period of time of between 8 hours to 18 hours, inclusive; drying the product at a room temperature; increasing the room temperature to a temperature between 100° C. and 120° C., inclusive, for a time period of between 8 hours to 12 hours, inclusive; and burning the product at a temperature of between 400° C. and 500° C., inclusive, for a time period of between 4 hours to 12 hours, inclusive.
 57. The catalytic composition according to claim 56, wherein the non-noble element from Group VIIIB of the periodic table comprises a concentration of between 5% and 25% by weight. 